Method of separation of hemicellulose and cellulose from polysaccharide sources

ABSTRACT

A method of separating hemicellulose and cellulose by dissolution of hemicellulose from a hemicellulose-rich source, such as a pulp of any origin or from holocellulose. In the method, hemicellulose is dissolved in a solvent system comprising a cellulose solvent, which is either a ionic liquid or another direct cellulose solvent, and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose, and wherein the solvent basicity and acidity of said ionic liquid or other direct cellulose solvent are adequately adjusted by the co-solvent. The present invention enables quantitative separation of cellulose and hemicellulose without any depolymerization and yield losses as occurring during conventional dissolving pulp manufacturing processes.

CROSS-REFERENCE TO RELATED APPLICATION

This application is entitled to the benefit of and incorporates by reference subject matter disclosed in International Patent Application No. PCT/FI2013/050414 filed on Apr. 15, 2013 and U.S. Provisional Patent Application No. 61/646,383 filed May 14, 2012.

FIELD OF INVENTION

The invention relates to the separation of hemicellulose and cellulose from polysaccharide sources. In particular, the present invention relates to methods of separating hemicelluloses and cellulose from hemicellulose-rich source, such as a pulp of any origin or from holocellulose by dissolution in suitable solvents. The present invention also relates to dissoloving pulps.

BACKGROUND

Dissolving pulp refers to pulp of high cellulose content which is used as raw material for the manufacture of cellulose derivatives and regenerated cellulose products. The wood-derived dissolving pulps which account for about 85% of the total dissolving pulp market are produced according to the acid sulphite and prehydrolysis-kraft (PHK) processes. In both cases additional purification steps such as hot and cold caustic extractions are necessary to achieve the requested degree of purification (determined as the content of residual hemicelluloses and alkali resistance). The removal of the hemicelluloses is associated with severe losses of cellulose mainly due to peeling-off reactions. Cellulose losses comprise between 15 and more than 30 wt-% depending on the process and the degree of purification. The removed hemicelluloses are largely converted to low molar mass hydroxy acids owing to alkaline post-extraction processes which constitutes another drawback of the current technologies. Cotton linters account for the residual 15% of the dissolving pulp market and represent the dissolving pulp of highest cellulose purity. They are particularly used for the production of acetate plastics and high-DP cellulose ethers.

Contrary to the paper pulp market, the dissolving pulp market shows a consistent annual growth of about 5% since the last ten years after the man-made cellulose fiber industry was consolidated during the 1990s. This growth is largely caused by the installation of new viscose fiber capacities in Asia but more and more also due to novel cellulose-based products requiring high purity dissolving pulps. At the same time the availability of cotton linters does not keep up with the increasing demand for several reasons.

It has been estimated that the annual demand of dissolving pulp will increase from currently 5-6 Mio t to about 12-20 Mio t in 2050, at least. This clearly underlines the need for novel environmentally friendly and economically attractive manufacturing processes for dissolving pulps of high purity which allow the concomitant recovery of hemicelluloses in high yield and purity.

SUMMARY

It is an aim of the present invention, to provide a means for selectively and (almost) quantitatively dissolved hemicelluloses from a hemicellulose-rich pulp of any origin as well as from holocellulose in an ionic liquid of which the solvent basicity and acidity are adequately adjusted by the addition of a co-solvent.

The solvent basicity and acidity are characterized by the Kamlet-Taft (KT) solubility parameters, primarily the b- (H-bond basicity) and α- (H-bond acidity) values, respectively.

Thus, the present invention concerns a method for separation of hemicellulose and cellulose by dissolution of hemicellulose from a hemicellulose-rich pulp of any origin or from holocellulose.

In the present method hemicellulose is dissolved in a solvent system comprising a cellulose solvent, which is either a ionic liquid or another direct cellulose solvent, and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose, and wherein the solvent basicity and acidity of said ionic liquid or other direct cellulose solvent are adequately adjusted by the co-solvent.

In an other aspect, this invention concerns a method for separation of hemicellulose and cellulose by dissolution of hemicellulose from a hemicellulose-rich pulp of any origin or from holocellulose, wherein hemicellulose is dissolved in a solvent system comprising a ionic liquid and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose and wherein the solvent basicity and acidity of said ionic liquid are adequately adjusted by the co-solvent.

In a third aspect, the present invention relates to dissolving pulps.

More specifically, the present method is mainly characterized by hemicellulose being dissolved in a solvent system comprising a cellulose solvent, which is either a ionic liquid or another direct cellulose solvent, and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose, and wherein the solvent basicity and acidity of said ionic liquid or other direct cellulose solvent are adequately adjusted by the co-solvent and wherein hemicellulose is dissolved in a solvent system comprising a ionic liquid and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose and wherein the solvent basicity and acidity of said ionic liquid are adequately adjusted by the co-solvent.

The dissolving pulps are characterized by cellulose pulp having a residual hemicellulose content of 1.0 to 10 wt-%, preferably between 2.0 and 5.0 wt-%.

Advantages

The present invention enables quantitative separation of cellulose and hemicellulose without any depolymerization and yield losses as occurring during conventional dissolving pulp manufacturing processes. The invention facilitates the integration of pulp refining into a cellulose regeneration process (IONCELL). Hemicelluloses are dissolved by a solvent system with adjusted solubility parameters instead of being fragmented by acid- or alkaline catalyzed degradation routes (acid sulfite process combined with hot caustic extraction or prehydrolysis kraft pulping with our without post-alkaline extraction).

Some important advantages are:

(a) Simple process, low energy consumption: dissolution treatment at slightly elevated temperature in a solvent system which is equally suited for cellulose, cellulose+hemicellulose or only hemicellulose dissolution. In this way this invention can be expanded to cellulose regeneration processes.

(b) No yield losses of both hemicellulose and cellulose: at the same level of cellulose purity, conventional prehydrolysis-kraft process experiences 5 to 10% cellulose yield loss on oven dry wood depending on the wood source and extent of cellulose purity. The same applies to the acid sulfite pulping process. Polymeric hemicelluloses cannot be recovered at all with the existing dissolving pulp manufacturing processes. However, the acid sulfite process allows to separate the dissolved monosugars from the sulfite spent liquor (SSL).

(c) The invention suggests the use of a cellulose solvent which can be also utilized in a conversion process, e.g. the cellulose regeneration process. This allows the combination of the pulp refining process (invention) with a fiber or film forming process using the dry-wet regeneration concept as suggested for the IONCELL process as mentioned above.

BRIEF DESCRIPTION OF DRAWINGS

The patent or application file contains at least one drawing executed in color. Copies of this patent or patent application publication with color drawing(s) will be provided by the Office upon request and payment of the necessary fee.

FIG. 1: shows a simplified scheme of fractionating a hemi-rich pulp into cellulose and hemicellulose fractions;

FIG. 2: shows cationic moieties of ionic liquids suitable of pulp dissolution;

FIG. 3: shows net basicity, (β−α), versus basicity (β) of [emim][OAc] mixed with increasing amount of co-solvent. The co-solvent is water. The Kamlet-Taft (KT) parameters have been determined at room temperature;

FIG. 4: shows glucan and xylan yields in the solid residue as a function of the water content. The results are expressed a wt-% on the amounts of glucan and xylan in the initial pulp;

FIG. 5: shows molar mass distribution of the initial bleached birch kraft pulp, the pulp residue (dissolving pulp, i.e. pure cellulose), the precipitate (extracted pure hemicellulose) and the calculated sum of the fractions. The treatment was carried out in [emim][OAc]-water with 15 wt-% water at 60° C. for 3 h; and

FIG. 6: shows molar mass distribution of the initial bleached pine kraft pulp, the pulp residue (dissolving pulp, i.e. cellulose), the precipitate (hemicellulose) and the calculated sum of the fractions. The treatment was carried out with [emim][OAc]-water with 15 wt-% water at 60° C. for 3 h.

DETAILED DESCRIPTION

As discussed above, the present technology provides a novel way of separating hemicellulose and cellulose by dissolution of hemicellulose from a hemicellulose-rich source in a solvent system comprising a cellulose solvent, which is either a ionic liquid or another direct cellulose solvent, together with a molecular solvent (co-solvent). The co-solvent is selected such that it does not dissolve cellulose. The solvent basicity and acidity of said ionic liquid or other direct cellulose solvent are adequately adjusted by the co-solvent.

The solvent basicity and acidity are characterized by the Kamlet-Taft solubility parameters, particularly by the β- (H-bond basicity) and α- (H-bond acidity) values.

To give some specific examples of preferred embodiment, in a first embodiment, the ionic liquid is a direct cellulose solvent, which has a cation selected from the group of cationic moieties depicted in FIG. 2, wherein the residues R₁₋₅ are independently linear or branched alkyl- (typically C1-C6), alkoxy-, or alkoxyalkyl groups, residues containing aryl moieties, or hydrogen, and an anion selected from the group consisting of halides (fluoride, chloride, bromide and iodide), pseudohalides (cyanide, thiocyanide, cyanate), carboxylates (formate, acetate, propionate, butyrate), alkyl sulphite, alkyl sulphate, trifluoromethane sulfonate, phenyl sulfonate, dialkyl phosphite, dialkyl phosphate, dialkyl phosphonites, and dialkyl phosphonates.

In a preferred embodiment, the ionic solvent has a net basicity (β−α) in the range 0.11-0.47; and a β-value in the range 0.57-0.95; preferably a net basicity (β−α) in the range 0.24-0.39; and a β-value in the range 0.70-0.88.

In the present technology, the ionic liquid can also be replaced by NMMO.H2O or LiCl/DMAc.

The co-solvent is preferably miscible with the ionic liquid. In particular, the co-solvent is capable of lowering the β-value and/or raising the α-value of the solvent system.

Preferably, the co-solvent is selected from the group consisting of water, methanol, ethanol, propanol, iso-propanol, butanol, acetone, acetonitrile, dimethylsulfoxide, dimethylformamide, dimethylacetamide and dimethylimidazolidione, preferably the co-solvent is water or ethanol.

In one particular embodiment, the co-solvent comprises another ionic liquid which itself is not capable of dissolving cellulose, so that this co-solvent-IL-mixture consists of an aforementioned cation and any anion not mentioned above, preferably of the type hexafluorophosphate, tetrafluoroborate, bis(trifluoromethane)sulfonimide.

Preferably, the ionic liquid is an [emim]-based ionic liquid.

Specific examples of ionic liquid are the following: [emim][OAc], [bmim][OAc], [emim][DMP] and [DEP], [DBNH][OAc], [DBNH][EtOAc], preferably [emim]OAc and [emim][DMP].

The co-solvent (to be combined with any of the above ionic liquids is water or an alcohol, preferably water, wherein the water content preferably is in the range 10-30 wt-%, and the solvent has a net basicity (β−α) in the range 0.11-0.47; and a β-value in the range 0.57-0.95; preferably a net basicity (β−α) in the range 0.24-0.39; and a β-value in the range 0.70-0.88.

The present method can be carried out, for example, at a temperature ranging from 20-150° C., preferably 40-80° C. for a time ranging from 10-400 min, preferably 60-180 min.

Pulp consistency can vary within broad ranges, typically being about 1-25 wt-%, preferably 5-15 wt-%.

The hemicellulose-rich pulp used as starting material can be any bleached or unbleached paper pulp of any lignocellulosic raw material derived from any commercial (sulphite, kraft, Soda-AQ) or non-commercial processes, such as organosolv, carboxylic acid, ASAM, ASA or MEA, although these examples are not exhaustive.

The dissolved hemicellulose fraction can be regenerated by the addition of a non-solvent, preferably water or alcohol, and the precipitate is separated by filtration or centrifugation.

In a further embodiment, the dissolved hemicellulose fraction is separated by pressure driven membrane processes, and/or a non-solvent is added to the hemicellulose-enriched retentate to initiate precipitation of the hemicellulose, and the hemicellulose is recovered as a pure powder after washing and drying.

Based on the above embodiments, a cellulose product can be obtained which has a residual hemicellulose content of 1.0 to 10 wt-%, preferably between 2.0 and 5.0 wt-%, and the isolated and purified hemicellulose has a residual cellulose content between 1.0 and 10 wt-%, preferably between 2.0 and 5 wt-%.

Typically, the cellulose and hemicellulose contents are calculated by the Janson formulae, and the neutral sugar contents are determined by HPAEC-PAD as described in reference [10].

The cellulose-rich residue can, for example, be dissolved in a cellulose solvent as mentioned above.

Modifications of the above methods are possible. Thus, for example oxidants or acids can be added to the cellulose dope to adjust the degree of polymerization suitable for the subsequent forming and regeneration processes. The amount of such oxidants or acids is typically 0.001 to 10% by weight of the total composition.

The oxidants added to the cellulose dope can be selected so as to be capable of removing chromophores such as residual lignin, HexA and extractives prior to the conversion processes.

The treated cellulose dope is subjected to filtration to remove undissolved impurities.

Turning now to the drawings, it can be noted that FIG. 1 shows a simplified scheme of the fractionation process. Thus, in the scheme, pulp was treated with a solvent system in a vertical kneader (or a stirrer at smaller scale) at various temperatures (60-80° C.) and retention times (0.5-6 h). The solvent system consisted of an [emim][OAc]-water mixture with a water content ranging between 10 wt-% and 30 wt-%. The resulting suspension was filtered (separated) with a press filter (or a centrifuge). The dissolved xylan was precipitated by further addition of water (non-solvent). The washed and dried cellulose and xylan fractions were analysed.

The solvent systems typically comprise an ionic liquid and a molecular solvent of which the latter is usually used in minor parts and, thus, can be stripped off easily to regenerate the ionic liquid. The herein presented concept is valid for all ionic liquids that were reported as cellulose solvents. This comprises in particular ionic liquids with cationic moieties such as depicted in FIG. 2. The residues R₁₋₅ are independently linear or branched alkyl- (typically C₁-C₆), alkoxy-, or alkoxyalkyl groups, residues containing aryl moieties, or hydrogen.

The preferred anions of the ionic liquids are halides (fluoride, chloride, bromide and iodide), pseudohalides (cyanide, thiocyanide, cyanate), carboxylates (formate, acetate, propionate, butyrate), alkyl sulphite, alkyl sulphate, trifluoromethane sulfonate, phenyl sulfonate, dialkyl phosphite, dialkyl phosphate, dialkyl phosphonites, dialkyl phosphonates (FIG. 2). Thus, the resulting ionic liquid is hydrophilic and its Kamlet-Taft basicity and net-basicity suitable for cellulose dissolution [7].

To generate a solvent system that allows aforementioned fractionation of holocellulose, the ionic liquid is mixed with a co-solvent. Any solvent that does not dissolve cellulose itself can be utilized as co-solvent to generate a selective solvent system. Preferred co-solvents are miscible with the respective ionic liquid and lower the b value (and/or raising the a value, respectively) of the resultant solvent mixture. Preferably, the co-solvent is water, methanol, ethanol, propanol, iso-propanol, butanol, acetone, acetonitrile, dimethylsulfoxide, dimethylformamide, dimethylacetamide, dimethylimidazolidione. The co-solvent can also comprise another ionic liquid which itself is not capable of dissolving cellulose. This co-solvent-IL consists of an aforementioned cation and and any anion not mentioned above, preferably of the type hexafluorophosphate, tetrafluoroborate, bis(trifluoromethane)sulfonimide. For environmental and energy saving reasons, water and ethanol are used more preferably.

In addition to ionic liquids also other direct cellulose solvents, preferably NMMO.H₂O and LiCl/DMAc, are suitable for the selective dissolution of low molar mass polysaccharides such as hemicelluloses or low molar mass cellulose from a hemicellulose-rich pulp when mixed with a co-solvent—as listed above—in a ratio so that the targeted solvent parameters (net basicity, b value) are adequately adjusted.

The Kamlet-Taft (KT) parameters have been proven to be useful solvent property indicators [1]. They are determined from the absorption peaks of the three dyes Reichardt's dye (RD, range 518-585 nm), N,N-diethyl-4-nitro-aniline (DENA, 402-414 nm) and 4-nitroaniline (NA, 406-398 nm). The peaks are typically fitted to a Gaussian function in order to precisely locate the maxima (v_(max)). From these functions v_(max)(T), the E_(T)(30), π*, α and β parameters are calculated using published equations [2].

Several authors have demonstrated that the H-bond basicity, expressed by the b-value, correlates with the capability of an ionic liquid to dissolve cellulose [2-6]. Other KT values were not found to correlate directly with the dissolution of cellulose.

Quite recently, we introduced the net basicity term, β−α, which allows a better prediction of both dissolution and regeneration of cellulose since it accounts for the acidity imparted by the cation or a protic co-solvent [7]. Based on a representative selection of cellulose solvents it was shown that cellulose dissolution generally conform to the requirement 0.35<β−α<0.9 with b>0.8 [7]. With the progressive addition of a protic co-solvent such as water or alcohol the H-bond basicity, b, decreases while the H-bond acidity, a, increases. This was demonstrated by adding water to [emim][OAc]. As shown in FIG. 3, the net basicity decreases faster than the b-value due to the opposite development of the b- and a-values with increasing amount of water in [emim][OAc]. Further, FIG. 3 reveals the ranges of the KT derived solubility parameters indicating complete and partial dissolution of hemicelluloses from paper-grade pulps.

As expected, the solubility of a hemicellulose-rich pulp decreases with an increasing percentage of water in an [emim][OAc]-water mixture when treated for three hours at about 60° C. in a vertical kneader.

Surprisingly, the extent of pulp dissolution decreases only gradually with increasing water concentration in [emim][OAc]. This was not expected since for some ionic liquids, e.g. for [bmim]Cl, the TMG-based ILs and others, it was known that the presence of only marginal amounts of water resulted in a complete stop of their capability to dissolve even fractions of a pulp [7][9]. The [emim][OAc]-water mixture, however, revealed high dissolution power even at relatively high water concentration. This was for example demonstrated for a bleached kraft pulp of which 60 wt-%, 28 wt-%, 20 wt-%, 13 wt-% and 1 wt-% were dissolved in [emim][OAc]-water mixtures with a water content of 10 wt-%, 15 wt-%, 20 wt-%, 25 wt-% and 30 wt-%, respectively. Beyond 30 wt-% water in [emim][OAc]-water dissolution of any pulp component stops.

A closer examination confirmed that the extent of dissolution and thus the dissolution power of the solvent system were mainly related to the molar mass of the pulp components. Factors such as the pulp morphology, supramolecular structure, degree of crystallinity and chemical properties (e.g. affecting hydrophilicity) of the pulp components are likely to affect the solution behaviour as well. The removal of pure hemicellulose and hemicellulose fractions from paper pulp was, however, unforeseeable despite the expected molar mass dependent pulp fractionation behavior of the [emim][OAc]-water solvent. The solvent properties of appropriate [emim][OAc]-water mixtures were obviously more favourable for the extraction of hemicellulose than for cellulose of comparable molar mass.

The results shown in FIG. 4 clearly indicate that xylan from a birch kraft pulp is most efficiently and selectively dissolved in [emim][OAc] containing 15-20 wt-% of water. Beside the water content of the solvent system, the efficiency and selectivity of hemicellulose dissolution were also affected by the dissolution conditions. This was demonstrated for a solvent mixture containing 20 wt-% of water. The results of different dissolution conditions for this particular water content of the solvent mixture are included in FIG. 4. The detailed results are presented in Example 3.

Based on the above, dissolving cellulose pulps are provided, wherein the cellulose pulps have a residual hemicellulose content of 1.0 to 10 wt-%.

Thus, a dissolving cellulose pulp obtained by a method as explained in the foregoing, in which the isolated and purified hemicelluloses is withdrawn from a hemicellulose-rich source, exhibits a residual cellulose content between 1.0 and 10 wt-%, preferably between 2.0 and 5 wt-%, the cellulose and hemicellulose contents being calculated by the Janson formulae, and the neutral sugar contents are determined by HPAEC-PAD as described in reference [10].

The following non-limiting Examples illustrate the invention,

EXAMPLE 1

Effect of the Water Content in [emim][OAc] on the Fractionation of a Commercial Birch Kraft Pulp: Composition of the Pulp Residue

ECF-bleached birch kraft pulp was treated with an [emim][OAc]-water mixture [10 wt-% to 30 wt-%] in a horizontal kneader for 3 h at 60° C. The subsequent phase separation was conducted with a filter press equipped with a metal fleece. The pore diameter was in the range 1-5 μm. The pulp residue was thoroughly washed with water, dried and subjected to analysis. Alternatively, the dissolution was supported by a stirrer and the phase separation by centrifugation. The results are summarized in Table 1.

TABLE 1 Effect of the water content in [emim][OAc] on the efficiency and selectivity of xylan removal. Characterization of the pulp residue. H₂O, Temp Xylan Viscosity Trial wt-% Consistency, % Conditions ° C. Time h Yield % content % mL/g Initial 100.0 23.1 808 Birch Pulp trial 3 10 3.3 kneader, 60 3 40.0 4.0 1040 filtration trial 1 15 3.3 kneader, 60 3 64.7 2.5 981 filtration trial 167 17.5 3.3 kneader, 60 3 76.1 3.9 954 filtration trial 164 20 3.3 kneader, 60 3 76.2 6.8 921 filtration trial 5 22.5 3.3 kneader, 60 3 90.0 9.6 886 filtration trial 2 25 3.3 kneader, 60 3 86.1 14.6 891 filtration trial 4 30 3.3 kneader, 60 3 98.8 21.4 808 filtration

EXAMPLE 2

Effect of the Water Content in [emim][OAc] on the Fractionation of a Commercial Birch Kraft Pulp: Composition of the Precipitated Soluble Fraction

The soluble fractions generated in Example 1 were precipitated by the addition of excess water (anti-solvent). The precipitated, extracted polysaccharides were centrifuged and washed thoroughly to remove the residual ionic liquid. The washed precipitates were dried at room temperature over night or, alternatively, by freeze drying. Table 2 shows the yield and the composition of the extracted low-molar mass pulp fractions.

TABLE 2 Effect of the water content in [emim][OAc] on the yield and purity of the extracted pulp fraction. Characterization of the precipitate from the soluble fraction. Mw (GPC) H₂O, Temp Cellulose* Pullulan Trial wt-% Consistency, % Conditions ° C. Time h Yield % content, % [kDa] Initial 0 Birch Pulp trial 3 10 3.3 kneader, 60 3 60.0 50.5  609.1  filtration trial 1 15 3.3 kneader, 60 3 35.3 3.7 23.4 filtration trial 167 17.5 3.3 kneader, 60 3 23.9 2.8 n.a. filtration trial 164 20 3.3 kneader, 60 3 23.8 n.a. n.a. filtration trial 5 22.5 3.3 kneader, 60 3 10.0 1.8 19.7 filtration trial 2 25 3.3 kneader, 60 3 13.9 2.0 21.9 filtration trial 4 30 3.3 kneader, 60 3 1.2 9.1 26.0 filtration *calculated according to the Janson formulae [8]

Table 2 shows that between a water content of 10 to 15 wt-% in [emim][OAc] the transition from cellulose/hemicellulose to pure hemicellulose extraction occurs. Thus, in the range between 15 wt-% and 25 wt-% of water basically only hemicellulose is extracted. Quantitative hemicellulose extraction is achieved in the range between 15 wt-% and 20 wt-% of water content in [emim][OAc] at least.

EXAMPLE 3

Effect of Dissolution Conditions at a Constant Water Content of 20 wt-% in [emim][OAc] on the Fractionation Efficiency and Selectivity of a Commercial Birch Kraft Pulp

In a series of experiments, where the water content was kept constant at 20 wt-% in [emim][OAc], the effects of temperature, time and mixing conditions on the fractionation of a bleached birch kraft pulp have been determined (table 3).

TABLE 3 Effect of temperature, time and mixing conditions at a water content of 20 wt- % in [emim][OAc] on the yield and purity of the pulp residue H₂O, Temp Xylan Viscosity Trial wt-% Consistency, % Conditions ° C. Time h Yield % content % mL/g Initial 0 Birch Pulp trial 164 20 3.3 kneader, 60 3 76.2 6.8 921 filtration trial 155 20 3.3 stirrer, 60 3 81.3 6.2 906 centrifuge trial 157 20 3.3 stirrer, 60 6 75.6 1.9 n.a. centrifuge trial 159 20 3.3 stirrer, 80 3 82.1 1.8 914 filtration trial 160 20 3.3 stirrer, 60 0.5 78.7 8.5 907 centrifuge trial 161 20 3.3 ultrasonication 60 3 80.2 1.5 920 trial 162 20 3.3 ultrasonication 60 6 79.6 1.8 n.a.

The support through longer retention time, higher temperature and the concomitant application of ultrasonication revealed a clear impact on the yield and purity of the pulp residue.

High temperature (80° C., 3 h) or moderate temperature combined with long dissolution time (60° C., 6 h) show significant better xylan dissolution efficiency as compared to standard conditions (60° C., 3 h). Further, the support of dissolution by ultrasonication seems to improve the efficiency/selectivity of xylan removal significantly. The xylan content of the pulp residue decreases to only 1.5 to 1.8% od, which fulfill the requirements for standard acetate grade pulps.

EXAMPLE 4

Effect of Pulp Consistency in the Solvent System [emim][OAc]-Water on the Fractionation Efficiency and Selectivity of a Commercial Birch Kraft Pulp.

Pulp consistency in a suspension or solution has an important impact on the economic feasibility of a process. Most experiments were conducted at a rather low consistency of 3.3 wt-% to facilitate the handling of the pulp-solvent system in the lab. The pulp consistency was increased to 10.5 wt-% in a separate experiment with bleached birch kraft pulp using [emim][OAc] with a water content of 15 wt-%. The results are compared with those achieved at a pulp consistency of only 3.3 wt-% in Table 4.

TABLE 4 Effect of pulp consistency at a water content of 15 wt-% in [emim][OAc] on the yield and purity of the pulp residue H₂O, Temp Xylan Viscosity Trial wt-% Consistency, % Conditions ° C. Time h Yield % content % mL/g Initial 0 Birch Pulp trial 1 15 3.3 kneader, 60 3 64.7 2.5 981 filtration trial 6 15 10.5 kneader, 60 3 73.1 2.7 969 filtration

Besides the yield of the residue, which was very difficult to determine, the performance at 10.5 wt-% consistency was comparable to that at 3.3 wt-% consistency (the yield of the former is more reliable considering mass balance). Evidence of the quantitative and highly selective fractionation of cellulose and hemicellulose from a hemicellulose-rich pulp has been provided by the comparative evaluation of the molar mass distributions of the initial pulp, the cellulose and hemicellulose fractions and their calculated sums. In this way it was shown that fractionation occurs in a highly selective and quantitative way. Thus, no degradation of cellulose or hemicellulose was observed as occurring during the conventional dissolving pulp processes.

EXAMPLE 5

Effect of Wood Raw Material: Birch vs. Pine Kraft Pulp

The fractionation performance of the solvent system [emim][OAc]-water with a water content of 15 wt-% was investigated for a pine kraft pulp in comparison to a birch kraft pulp. The results are summarized in Table 5.

TABLE 5 Effect of wood raw material of a paper grade kraft pulp on the yield and purity of the pulp residue. Treatment conditions: 85 wt-% [emim][OAc] + 15 wt-% water, 60° C., 3 h in a kneader, phase separation with a press filter H₂O, Temp Cellulose, Xylan GGM Viscosity Trial wt-% Consistency, % ° C. Time, h Yield % %* %* %* mL/g Initial birch 100.0 70.3 28.7 1.0 808 pulp treated 15 3.3 60 3 64.7 96.7 3.3 0.0 981 birch pulp, trial 1 Initial pine 100.0 82.3 9.7 8.0 832 pulp treated 15 3.3 60 3 77.5 96.2 1.5 2.3 932 pine pulp, trial 7 *calculated according to the Janson formulae [8]

The successful separation of cellulose and hemicelluloses from a pine kraft pulp is also reflected in their molar mass distributions (FIG. 6). From the results it can be concluded that softwood and hardwood kraft pulps are equally suited as substrate for the quantitative separation of hemicellulose and cellulose by applying the process according to the present invention.

Examples 1-5 confirm the viability of the novel fractionation concept of hemicellulose-rich pulps (holocellulose, paper-grade pulps) using an IL-co-solvent mixture with suitable solvent parameters as expressed by the KT-parameters and appropriate dissolution conditions (FIG. 3).

With reference to work on the dissolution of cellulose [7] conditions can now be proposed allowing the complete and partial dissolution of hemicelluloses from hemicellulose-rich polysaccharides, preferred from bleached paper grade pulps.

FIG. 3 shows the solubility window for the complete (β−α=0.24−0.39; β=0.70−0.88) and the complete and partial (β−α=0.11−0.47; β=0.57−0.95) dissolution of hemicelluloses.

The appropriate solvent properties have been conveniently adjusted by the addition of water to [emim][OAc]. However, the fractionation concept can be successfully transferred to any cellulose solvent-co-solvent mixture provided that the solubility parameters fulfil the requirements as defined for the hemicellulose dissolution window (complete and partial).

Different to conventional and novel fractionation schemes for the manufacture of dissolving pulp using chemical reactions, the proposed invention allows a quantitative separation of hemicelluloses and cellulose of high purity without any losses and the depolymerisation of the associated polymers.

Supporting the extraction by high intensity mixing at elevated temperature promotes the fractionation efficiency and selectivity as exemplified in Table 3.

Quantitative separation of cellulose and hemicellulose of hemicellulose-rich pulps or holocellulose, is embedded in a new process concept, IONCELL, which, as a first step, comprises the separation of the hemicellulose from the original hemicellulose-rich substrate. Step 2 of the IONCELL process is characterized by the separation of the dissolved hemicellulose after phase separation. The separation is preferentially conducted by membrane separation to avoid any further dilution of the solvent (e.g. ionic liquid).

Alternatively, the addition of a non-solvent, preferably equivalent to the co-solvent (e.g. water), is added to the solution to precipitate the hemicellulose (FIG. 1). An appropriate filtration of the generated hemicellulose/solvent/co-solvent suspension ensures a quantitative phase separation. The filtrated hemicellulose is washed and dried while the solvent/non-solvent mixture is recycled to the fractionation process after the co-solvent content has been adjusted to the desired value.

In a third step, the purified cellulose fraction is dissolved in a cellulose solvent, e.g. ionic liquid, recycled either from the conversion (fibre, film) or from the fractionation process. The dope may be further treated by oxidants (bleaching chemicals like hydrogen peroxide, ozone and others) to remove impurities (bleaching) in the case of an unbleached pulp as initial substrate and/or to adjust the degree of polymerization as requested by subsequent forming and regeneration processes. Those processes comprise primarily the production of regenerated fibers and films.

While the present invention has been illustrated and described with respect to a particular embodiment thereof, it should be appreciated by those of ordinary skill in the art that various modifications to this invention may be made without departing from the spirit and scope of the present. 

What is claimed is:
 1. A method of separating hemicellulose and cellulose by dissolution of hemicellulose from a hemicellulose-rich source, such as a pulp of any origin or from holocellulose, characterized in that wherein hemicellulose is dissolved in a solvent system comprising a cellulose solvent, which is either a ionic liquid or another direct cellulose solvent, and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose, and wherein the solvent basicity and acidity of said ionic liquid or other direct cellulose solvent are adequately adjusted by the co-solvent.
 2. The method according to claim 1, characterized in that wherein hemicellulose is dissolved in a solvent system comprising a ionic liquid and a molecular solvent (co-solvent), wherein said co-solvent does not dissolve cellulose and wherein the solvent basicity and acidity of said ionic liquid are adequately adjusted by the co-solvent.
 3. The method according to claim 1, wherein the solvent basicity and acidity are characterized by the Kamlet-Taft solubility parameters, particularly by the β- (H-bond basicity) and α- (H-bond acidity) values.
 4. The method according to claim 1, wherein said co-solvent is miscible with the ionic liquid.
 5. The method according to claim 1, wherein said co-solvent is capable of lowering the β-value and/or raising the α-value of the solvent system.
 6. The method according to claim 1, wherein i) the ionic liquid is a direct cellulose solvent, which preferably has a cation selected from the group of cationic moieties depicted in FIG. 2, wherein the residues R₁₋₅ are independently linear or branched alkyl- (typically C1-C6), alkoxy-, or alkoxyalkyl groups, residues containing aryl moieties, or hydrogen, and an anion selected from the group consisting of halides (fluoride, chloride, bromide and iodide), pseudohalides (cyanide, thiocyanide, cyanate), carboxylates (formate, acetate, propionate, butyrate), alkyl sulphite, alkyl sulphate, trifluoromethane sulfonate, phenyl sulfonate, dialkyl phosphite, dialkyl phosphate, dialkyl phosphonites, and dialkyl phosphonates, or ii) the ionic liquid is replaced by NMMO.H₂O or LiCl/DMAc.
 7. The method according to claim 1, wherein the co-solvent is selected from the group consisting of water, methanol, ethanol, propanol, iso-propanol, butanol, acetone, acetonitrile, dimethylsulfoxide, dimethylformamide, dimethylacetamide and dimethylimidazolidione, preferably the co-solvent is water or ethanol.
 8. The method according to claim 1, wherein the co-solvent comprises another ionic liquid which itself is not capable of dissolving cellulose, so that this co-solvent-IL-mixture consists of an aforementioned cation and any anion not mentioned above, preferably of the type hexafluorophosphate, tetrafluoroborate, bis(trifluoromethane)sulfonimide.
 9. The method according to claim 1, wherein the ionic solvent has a net basicity (β−α) in the range 0.11-0.47; and a β-value in the range 0.57-0.95; preferably a net basicity (β−α) in the range 0.24-0.39; and a β-value in the range 0.70-0.88.
 10. The method according to claim 1, wherein the ionic liquid is an [emim]-based ionic liquid.
 11. The method according to claim 1, wherein the ionic liquid is [emim][OAc], [bmim][OAc], [emim][DMP], [DEP], [DBNH][OAc], [DBNH][EtOAc], preferably [emim]OAc, or [emim][DMP], the co-solvent is water or an alcohol, preferably water, wherein the water content preferably is in the range 10-30 wt-%, and the solvent has a net basicity (β−α) in the range 0.11-0.47; and a β-value in the range 0.57-0.95; preferably a net basicity (β−α) in the range 0.24-0.39; and a β-value in the range 0.70-0.88.
 12. The method according to claim 1, wherein the method is carried out at a temperature ranging from 20-150° C., preferably 40-80° C. for a time ranging from 10-400 min, preferably 60-180 min.
 13. The method according to claim 1, wherein the pulp consistency is 1-25 wt-%, preferably 5-15 wt-%.
 14. The method according to claim 1, wherein the hemicellulose-rich pulp used as starting material is bleached or unbleached paper pulp of any lignocellulosic raw material derived from any commercial (sulphite, kraft, Soda-AQ) or non-commercial processes, such as organosolv, carboxylic acid, ASAM, ASA or MEA.
 15. The method according to claim 1, wherein the dissolved hemicellulose fraction is regenerated by the addition of a non-solvent, preferably water or alcohol, and the precipitate is separated by filtration or centrifugation.
 16. The method according to claim 1, wherein the dissolved hemicellulose fraction is separated by pressure driven membrane processes, and/or a non-solvent is added to the hemicellulose-enriched retentate to initiate precipitation of the hemicellulose, and the hemicellulose is recovered as a pure powder after washing and drying.
 17. The method according to claim 1, wherein the final cellulose product obtained has a residual hemicellulose content of 1.0 to 10 wt-%, preferably between 2.0 and 5.0 wt-%, and the isolated and purified hemicellulose has a residual cellulose content between 1.0 and 10 wt-%, preferably between 2.0 and 5 wt-%, wherein the cellulose and hemicellulose contents are calculated by the Janson formulae, and the neutral sugar contents are determined by HPAEC-PAD as described in reference [10].
 18. The method according to claim 1, wherein the cellulose-rich residue is dissolved in a cellulose solvent.
 19. The method according to claim 1, wherein oxidants or acids are added to the cellulose dope to adjust the degree of polymerization suitable for the subsequent forming and regeneration processes.
 20. The method according to claim 1, wherein oxidants are added to the cellulose dope to remove chromophores such as residual lignin, HexA and extractives prior to the conversion processes.
 21. The method according to claim 17, wherein the treated cellulose dope is subjected to filtration to remove undissolved impurities.
 22. A dissolving cellulose pulp, obtained by a method according to claim 1, wherein said cellulose pulp has a residual hemicellulose content of 1.0 to 10 wt-%, preferably between 2.0 and 5.0 wt-%.
 23. The dissolving cellulose pulp according to claim 22, obtained by a method in which the isolated and purified hemicellulose, withdrawn from a hemicellulose-rich source, has a residual cellulose content between 1.0 and 10 wt-%, preferably between 2.0 and 5 wt-%, and wherein the cellulose and hemicellulose contents are calculated by the Janson formulae, and the neutral sugar contents are determined by HPAEC-PAD. 